CN114478171A - Method and system for refining cumene - Google Patents
Method and system for refining cumene Download PDFInfo
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- CN114478171A CN114478171A CN202011156375.9A CN202011156375A CN114478171A CN 114478171 A CN114478171 A CN 114478171A CN 202011156375 A CN202011156375 A CN 202011156375A CN 114478171 A CN114478171 A CN 114478171A
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- cumene
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- RWGFKTVRMDUZSP-UHFFFAOYSA-N cumene Chemical compound CC(C)C1=CC=CC=C1 RWGFKTVRMDUZSP-UHFFFAOYSA-N 0.000 title claims abstract description 524
- 238000000034 method Methods 0.000 title claims abstract description 63
- 238000007670 refining Methods 0.000 title claims abstract description 21
- 238000011084 recovery Methods 0.000 claims abstract description 91
- 239000012535 impurity Substances 0.000 claims abstract description 69
- 239000007788 liquid Substances 0.000 claims abstract description 7
- 239000002994 raw material Substances 0.000 claims abstract description 7
- 238000007599 discharging Methods 0.000 claims abstract description 6
- 238000000605 extraction Methods 0.000 claims abstract 2
- GOOHAUXETOMSMM-UHFFFAOYSA-N Propylene oxide Chemical compound CC1CO1 GOOHAUXETOMSMM-UHFFFAOYSA-N 0.000 claims description 14
- FRIBMENBGGCKPD-UHFFFAOYSA-N 3-(2,3-dimethoxyphenyl)prop-2-enal Chemical compound COC1=CC=CC(C=CC=O)=C1OC FRIBMENBGGCKPD-UHFFFAOYSA-N 0.000 claims description 12
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 claims description 6
- BDCFWIDZNLCTMF-UHFFFAOYSA-N 2-phenylpropan-2-ol Chemical compound CC(C)(O)C1=CC=CC=C1 BDCFWIDZNLCTMF-UHFFFAOYSA-N 0.000 claims description 3
- 239000007795 chemical reaction product Substances 0.000 claims description 2
- 238000002360 preparation method Methods 0.000 claims description 2
- 239000007789 gas Substances 0.000 claims 8
- 238000000926 separation method Methods 0.000 abstract description 18
- 238000007254 oxidation reaction Methods 0.000 abstract description 9
- 239000003054 catalyst Substances 0.000 abstract description 7
- 238000005265 energy consumption Methods 0.000 abstract description 4
- WVDDGKGOMKODPV-UHFFFAOYSA-N Benzyl alcohol Chemical compound OCC1=CC=CC=C1 WVDDGKGOMKODPV-UHFFFAOYSA-N 0.000 description 33
- 239000000203 mixture Substances 0.000 description 15
- JESIHYIJKKUWIS-UHFFFAOYSA-N 1-(4-Methylphenyl)ethanol Chemical compound CC(O)C1=CC=C(C)C=C1 JESIHYIJKKUWIS-UHFFFAOYSA-N 0.000 description 13
- 229920000642 polymer Polymers 0.000 description 13
- 238000006243 chemical reaction Methods 0.000 description 12
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 description 12
- 235000019445 benzyl alcohol Nutrition 0.000 description 11
- 239000001257 hydrogen Substances 0.000 description 8
- 229910052739 hydrogen Inorganic materials 0.000 description 8
- 239000000463 material Substances 0.000 description 7
- 230000000052 comparative effect Effects 0.000 description 6
- 238000004519 manufacturing process Methods 0.000 description 6
- 239000007858 starting material Substances 0.000 description 6
- 239000000945 filler Substances 0.000 description 5
- 230000003647 oxidation Effects 0.000 description 5
- 239000000047 product Substances 0.000 description 5
- DNIAPMSPPWPWGF-UHFFFAOYSA-N Propylene glycol Chemical compound CC(O)CO DNIAPMSPPWPWGF-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 238000006735 epoxidation reaction Methods 0.000 description 3
- 150000002431 hydrogen Chemical class 0.000 description 3
- 238000006116 polymerization reaction Methods 0.000 description 3
- HGTUJZTUQFXBIH-UHFFFAOYSA-N (2,3-dimethyl-3-phenylbutan-2-yl)benzene Chemical compound C=1C=CC=CC=1C(C)(C)C(C)(C)C1=CC=CC=C1 HGTUJZTUQFXBIH-UHFFFAOYSA-N 0.000 description 2
- LYCAIKOWRPUZTN-UHFFFAOYSA-N Ethylene glycol Chemical compound OCCO LYCAIKOWRPUZTN-UHFFFAOYSA-N 0.000 description 2
- XENVCRGQTABGKY-ZHACJKMWSA-N chlorohydrin Chemical compound CC#CC#CC#CC#C\C=C\C(Cl)CO XENVCRGQTABGKY-ZHACJKMWSA-N 0.000 description 2
- 238000005260 corrosion Methods 0.000 description 2
- 230000007797 corrosion Effects 0.000 description 2
- 125000002592 cumenyl group Chemical group C1(=C(C=CC=C1)*)C(C)C 0.000 description 2
- 230000007547 defect Effects 0.000 description 2
- 238000007327 hydrogenolysis reaction Methods 0.000 description 2
- 238000012856 packing Methods 0.000 description 2
- 230000000379 polymerizing effect Effects 0.000 description 2
- 239000011148 porous material Substances 0.000 description 2
- 238000010992 reflux Methods 0.000 description 2
- 239000000126 substance Substances 0.000 description 2
- 238000009489 vacuum treatment Methods 0.000 description 2
- NLHHRLWOUZZQLW-UHFFFAOYSA-N Acrylonitrile Chemical compound C=CC#N NLHHRLWOUZZQLW-UHFFFAOYSA-N 0.000 description 1
- 239000004721 Polyphenylene oxide Substances 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- XYLMUPLGERFSHI-UHFFFAOYSA-N alpha-Methylstyrene Chemical group CC(=C)C1=CC=CC=C1 XYLMUPLGERFSHI-UHFFFAOYSA-N 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 238000004821 distillation Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- WGCNASOHLSPBMP-UHFFFAOYSA-N hydroxyacetaldehyde Natural products OCC=O WGCNASOHLSPBMP-UHFFFAOYSA-N 0.000 description 1
- 239000002736 nonionic surfactant Substances 0.000 description 1
- 239000000575 pesticide Substances 0.000 description 1
- 239000003208 petroleum Substances 0.000 description 1
- 229920000570 polyether Polymers 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 125000004805 propylene group Chemical group [H]C([H])([H])C([H])([*:1])C([H])([H])[*:2] 0.000 description 1
- 239000004753 textile Substances 0.000 description 1
- 238000005292 vacuum distillation Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C7/00—Purification; Separation; Use of additives
- C07C7/04—Purification; Separation; Use of additives by distillation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
- B01D3/14—Fractional distillation or use of a fractionation or rectification column
- B01D3/143—Fractional distillation or use of a fractionation or rectification column by two or more of a fractionation, separation or rectification step
Abstract
The invention discloses a method and a system for refining cumene, which comprises the following steps: step 1, rectifying a stream containing cumene, discharging light components from the top of a tower, and extracting the cumene from a side line; and 2, further rectifying the tower bottom liquid obtained in the step 1, circulating the tower top stream to the step 1 as a raw material, and discharging the tower bottom liquid. The system sequentially comprises a cumene recovery tower and a cumene circulating tower according to a feeding sequence, wherein a cumene side line extraction position is arranged at the middle upper part of the cumene recovery tower, a tower kettle of the cumene recovery tower is connected with a feeding hole of the cumene circulating tower, and the tower top of the cumene circulating tower is connected with the feeding hole of the cumene recovery tower. The method or the system ensures the separation of impurities such as isopropyl benzene, AMS and the like, ensures that the concentration of the refined isopropyl benzene meets the feeding requirement of the oxidation reaction, prevents the impurities from damaging a catalyst and an equipment pipeline, and simultaneously reduces the energy consumption in the separation process.
Description
Technical Field
The invention relates to the refining of isopropyl benzene, in particular to a method for refining an isopropyl benzene stream obtained in a benzyl alcohol conversion procedure in a technology for preparing epoxy propane by a CHP method.
Background
The propylene oxide is used as an important organic raw material, can be used for producing polyether glycol, propylene glycol, various nonionic surfactants and the like, and is widely applied to industries such as petroleum, chemical industry, pesticides, textile and the like. Propylene oxide is a propylene derivative that is produced second only to polypropylene and acrylonitrile and is in increasing demand as its use and demand continue to increase.
Current methods for producing propylene oxide include the chlorohydrin process, the co-oxidation process (co-production), and the cumene hydroperoxide process (CHP process, without co-production). The chlorohydrin method has mature process, but has the defects of large water consumption, more three wastes, equipment corrosion and the like; the co-oxidation method has less pollution and low product cost, but has the defects of long process, high investment, influence of the co-product market and the like. The CHP method has no co-production, low investment, small pollution and no corrosion to equipment, and is a popular propylene oxide production method at present.
The CHP method for producing the propylene oxide mainly comprises an oxidation process, an epoxidation process, a product refining process and a benzyl alcohol conversion process. The epoxidation procedure obtains crude propylene oxide and a mixture containing alpha, alpha-dimethyl benzyl alcohol (DMBA) and the like; the crude epoxypropane is subjected to a product refining procedure to obtain an epoxypropane product; the mixture containing DMBA enters a benzyl alcohol conversion procedure to obtain isopropyl benzene; the cumene is circulated to the oxidation procedure to obtain the cumene hydroperoxide for the epoxidation procedure, thereby realizing the cumene circulation.
In the benzyl alcohol conversion procedure, the mixture containing DMBA and hydrogen are subjected to hydrogenolysis reaction under the action of a catalyst to obtain a mixture containing cumene. Wherein the mixture mainly comprises isopropyl benzene, hydrogen, methane, AMS, DMBA, polymer and the like. The cumene-containing mixture does not meet the requirements of an oxidation procedure on raw material cumene because of high impurity content; and if the substances such as polymers and the like are not removed in time, accumulation can be formed in the system, catalyst pore channels and equipment pipelines are easy to block, and the activity of the catalyst and the safety of equipment are influenced. Therefore, the cumene mixture obtained in the benzyl alcohol conversion step is purified and then recycled to the oxidation step.
Disclosure of Invention
In order to overcome the problems in the prior art, the invention provides a method for refining cumene, which can remove heavy components out of a propylene oxide production system and has the characteristics of simple flow, high cumene recovery rate, easiness in implementation and the like.
One of the objects of the present invention is to provide a method for purifying cumene, comprising the steps of:
and 2, further rectifying the tower bottom liquid obtained in the step 1, circulating the tower top stream to the step 1 as a raw material, and discharging the tower bottom liquid.
After being refined by the method, the cumene containing impurities is circulated to the oxidation process of preparing the propylene oxide by the CHP method and is used for producing the cumene hydroperoxide.
In a preferred embodiment, the stream containing cumene in step 1 is the reaction product of alpha, alpha dimethyl benzyl alcohol (DMBA) and hydrogen (in the benzyl alcohol conversion process) in the CHP (cumene hydroperoxide) process for making propylene oxide.
In a further preferred embodiment, the cumene-containing stream in step 1 contains cumene, light component impurities and heavy component impurities.
Wherein the light component impurities comprise hydrogen, methane and the like, the heavy component impurities comprise 2-phenyl-1 propylene (AMS), alpha dimethyl benzyl alcohol (DMBA), polymers and the like, and the related polymers mainly comprise 2, 3-dimethyl-2, 3-diphenyl butane (CAS: 1889-67-4) and the like.
In a further preferred embodiment, in the cumene-containing stream, the weight contents of the components are: cumene 90 to 100 wt% (preferably 95 to 100 wt%, and not including 100 wt%), light component impurities 0 to 2.5 wt% (preferably 0 to 1.25 wt%), and heavy component impurities 0 to 7.5 wt% (preferably 0 to 3.75 wt%).
The cumene content does not include 100%, i.e., the content of at least one of light component impurities and heavy component impurities is not 0 wt%.
Specifically, the raw material of the method is the discharge of a hydrogenolysis reactor in the conversion process of benzyl alcohol in the preparation of propylene oxide from CHP.
In a preferred embodiment, in step 1, the pressure of the rectification treatment is controlled to be 0.01 to 0.15MPaG, preferably 0.03 to 0.12 MPaG.
In a more preferred embodiment, in step 1, the pressure of the rectification treatment is controlled to be 0.04 to 0.10MPaG, preferably 0.04 to 0.09 MPaG.
For example, the operating pressure of the rectification treatment in step 1 is controlled to be 0.03MPaG, 0.04MPaG, 0.05MPaG, 0.06MPaG, 0.07MPaG, 0.08MPaG, 0.09MPaG, 0.10MPaG, 0.11MPaG, 0.12 MPaG.
In a preferred embodiment, in the rectification treatment in the step 1, the temperature of the top of the tower is controlled to be 100-210 ℃, and/or the temperature of the bottom of the tower is controlled to be 130-280 ℃.
In a further preferred embodiment, in the rectification treatment in the step 1, the tower top temperature is controlled to be 120-180 ℃, preferably 140-160 ℃; and/or controlling the temperature of the tower kettle to be 160-260 ℃, preferably 170-200 ℃.
In the step 1, a mixture of light component impurities is obtained at the tower top, and a cumene mixture containing heavy component impurities is obtained at the tower bottom.
In a preferred embodiment, the rectification in step 1 is carried out with a theoretical plate number of 20 to 70, preferably 30 to 60.
In a further preferred embodiment, the cumene is taken off in a side stream at a theoretical plate (from top to bottom) of 10 to 30, preferably at a theoretical plate (from top to bottom) of 15 to 25, when the rectification in step 1 is carried out.
In a further preferred embodiment, in carrying out the rectification described in step 1, the feed is carried out at from 25 to 41 (from top to bottom) theoretical plates, preferably from 30 to 35 (from top to bottom) theoretical plates.
Wherein, cumene of 70-100 wt%, preferably 99.8-100 wt% (recovery rate) in the raw material is extracted from the side line in the step 1 (based on the weight of the fresh feed in the step 1).
According to the invention, the isopropyl benzene and impurities are firstly subjected to the first rectification treatment in the step 1, high-purity isopropyl benzene is extracted from the side line, and a small amount of heavy component mixture containing the isopropyl benzene is subjected to the second rectification treatment in the step 2, so that the operating temperature of the first rectification treatment is reduced.
In a preferred embodiment, the rectification in step 2 is carried out under vacuum.
In a further preferred embodiment, the pressure of the rectification treatment in step 2 is controlled to be-0.09 to-0.01 MPaG, preferably-0.09 to-0.04 MPaG.
In a further preferred embodiment, the pressure of the rectification treatment in step 2 is controlled to be-0.09 to-0.05 MPaG, more preferably-0.09 to-0.06 MPaG.
For example, the operating pressure of the rectification treatment described in step 2 is-0.09 MPaG, -0.08MPaG, -0.07MPaG, -0.06MPaG, -0.05MPaG, -0.04 MPaG.
In a preferred embodiment, in the rectification treatment in the step 2, the temperature of the top of the tower is controlled to be 80-160 ℃, preferably 100-150 ℃, and/or the temperature of the bottom of the tower is controlled to be 150-240 ℃, preferably 140-230 ℃.
Wherein, the step 2 adopts vacuum treatment, thus reducing the treatment temperature and avoiding the heavy components from polymerizing at high temperature.
In a preferred embodiment, when the rectification in step 2 is carried out, the number of theoretical plates is 10 to 50, preferably 10 to 30.
In a further preferred embodiment, in the rectification in step 2, the feed is carried out at 5 to 20 (from top to bottom) theoretical plates, preferably at 5 to 10 (from top to bottom) theoretical plates.
In the rectification treatment in the step 2, 99 to 100 wt% of cumene in the tower bottom liquid obtained in the step 1 is extracted from the tower top (calculated as 100 wt% of cumene in the feeding material in the step 2), and 99 to 100 wt% of heavy component impurities in the feeding material of the cumene circulation tower are extracted from the tower bottom (calculated as 100 wt% of heavy component impurities in the feeding material in the step 2). The heavy component impurities include AMS, DMBA, polymers, and the like.
The invention also aims to provide a cumene refining system which sequentially comprises a cumene recovery tower and a cumene circulating tower according to the feeding sequence, wherein a cumene side draw-out position is arranged at the middle upper part of the cumene recovery tower, a tower kettle of the cumene recovery tower is connected with a feeding hole of the cumene circulating tower, and the tower top of the cumene circulating tower is connected with the feeding hole of the cumene recovery tower.
In a preferred embodiment, the cumene recovery column and/or the cumene recycle column is selected from the group consisting of a rectification column.
In a further preferred embodiment, the cumene recovery column is an atmospheric distillation column, and the cumene recycle column is a vacuum distillation column.
In a preferred embodiment, the theoretical plate number of the cumene recovery column is 20 to 70, preferably 30 to 60.
In a further preferred embodiment, in the cumene recovery column, the cumene side draw is disposed at a theoretical plate of 10 to 30, preferably at a theoretical plate of 15 to 25.
In a further preferred embodiment, the cumene recovery column is fed at a position of from 25 to 41 theoretical plates, preferably from 30 to 35 theoretical plates.
In the invention, the cumene recovery tower can adopt a rectifying tower in the prior art, and can be a plate tower or a packed tower.
In a preferred embodiment, a light component outlet is provided at the top of the cumene recovery column.
In a further preferred embodiment, a heavy component outlet is provided in the bottom of the cumene recovery column, and the heavy component outlet is connected to the feed inlet of the cumene recycle column.
In a preferred embodiment, the cumene recovery column has a pressure of 0.01 to 0.15MPaG, preferably 0.03 to 0.12 MPaG.
In a further preferred embodiment, the cumene recovery column has a pressure of 0.04 to 0.10MPaG, preferably 0.04 to 0.09 MPaG.
In a preferred embodiment, the temperature of the top of the cumene recovery tower is 100 to 210 ℃, and/or the temperature of the bottom of the tower is controlled to be 130 to 280 ℃.
In a further preferred embodiment, the temperature of the top of the cumene recovery column is 120 to 180 ℃ and/or the temperature of the bottom of the column is controlled to 160 to 260 ℃.
In a further preferred embodiment, the temperature of the top of the cumene recovery column is 140 to 160 ℃, and/or the temperature of the bottom of the column is controlled to 170 to 200 ℃.
In a preferred embodiment, the cumene recycle column is a vacuum column.
In a further preferred embodiment, the cumene recycle column has a pressure of-0.09 to-0.01 MPaG, preferably-0.09 to-0.04 MPaG.
In a further preferred embodiment, the pressure of the rectification in step 2 is between-0.09 and-0.05 MPaG, more preferably between-0.09 and-0.06 MPaG.
For example, the operating pressure of the rectification treatment described in step 2 is-0.09 MPaG, -0.08MPaG, -0.07MPaG, -0.06MPaG, -0.05MPaG, -0.04 MPaG.
In a preferred embodiment, the temperature of the top of the cumene circulating tower is 80-160 ℃, preferably 100-150 ℃, and/or the temperature of the bottom of the tower is controlled to be 150-240 ℃, preferably 140-230 ℃.
Wherein, the step 2 adopts vacuum treatment, thus reducing the treatment temperature and avoiding the heavy components from polymerizing at high temperature.
In a preferred embodiment, the number of theoretical plates of the cumene recycle column is 10 to 50, preferably 10 to 30.
In a preferred embodiment, the cumene recycle column is fed at 5 to 20 theoretical plates, preferably 5 to 10 theoretical plates.
In a preferred embodiment, a recycle cumene outlet is provided at the top of the cumene recycle column, and the recycle cumene outlet is connected to the feed port of the cumene recovery column.
In the invention, the cumene circulating tower can adopt a rectifying tower in the prior art, and can be a plate tower or a packed tower.
According to the invention, the cumene and impurities are firstly separated in the cumene recovery tower, high-purity cumene is extracted from the side line of the cumene recovery tower, a small amount of mixture containing the cumene is treated in the cumene circulating tower, and the operating temperature of the cumene recovery tower is reduced. The cumene circulating tower adopts a vacuum tower, can effectively control the operating temperature of the cumene circulating tower, reduces the energy consumption of a system, and simultaneously reduces the possibility of polymerization of AMS and cumene in a tower kettle.
In the invention, the cumene is only extracted from the cumene recovery tower, so the ratio of the mass flow of the cumene extracted from the side line of the cumene recovery tower to the mass flow of the cumene in the fresh feed of the cumene recovery tower is defined as the recovery rate (R) of the cumene, and the formula is as follows:
in the formula F0’(cumene) is the cumene mass flow in the side line withdrawal stream of the cumene column; f0The (cumene) is the mass flow of cumene in the fresh feed of the cumene recovery column.
In the invention, the light component impurities are only extracted from the cumene recovery tower, so that the ratio of the mass flow of the light component impurities extracted from the top of the cumene recovery tower to the mass flow of the light component impurities in the fresh feed of the cumene recovery tower defines the removal rate (W) of the light component impurities1) The formula is as follows:
in the formula F0’Mass flow of each light component impurity in the stream extracted from the top of the cumene recovery tower; f0For cumene recoveryAnd (4) collecting the mass flow of each light component impurity in the fresh feed of the tower.
In the invention, the heavy component impurities are only extracted from the cumene circulating tower, so the ratio of the mass flow of the heavy component impurities extracted from the tower kettle of the cumene circulating tower to the mass flow of the heavy component impurities in the fresh feed of the cumene recovery tower T1 defines the removal rate of the heavy component impurities (W2) The formula is as follows:
in the formula F0’The mass flow of each impurity in the stream extracted from the tower kettle of the cumene circulating tower is measured; f0The mass flow of each impurity in fresh feed for the cumene recovery column.
The endpoints of the ranges and any values disclosed in the present application are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual values, and between the individual values may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein. In the above, the various technical solutions can in principle be combined with each other to obtain a new technical solution, which should also be considered as specifically disclosed in the present invention.
Compared with the prior art, the invention has the following beneficial effects: the method or the system ensures the separation of impurities such as isopropyl benzene, AMS and the like, ensures that the concentration of the refined isopropyl benzene meets the feeding requirement of the oxidation reaction, prevents the impurities from damaging a catalyst and an equipment pipeline, and simultaneously reduces the energy consumption in the separation process. By the refining method, the removal rate W of light component impurities such as hydrogen, methane and the like199.99 percent, and the removal rate W of heavy component impurities such as AMS, DMBA, polymer and the like299.99 percent, the recovery rate R of the isopropyl benzene is as high as 99.99 percent, and the refining effect is good.
Drawings
Fig. 1 shows a schematic of the system of the present invention.
In fig. 1, T1 is a cumene recovery column, T2 is a cumene recycle column, 1 is a fresh stream of a mixture containing cumene, 2 is a light component impurity stream withdrawn from the top of the cumene recovery column T1, 3 is a side draw stream of the cumene recovery column T1, 4 is a bottom draw stream of the cumene recovery column T1, 5 is a recycle cumene stream withdrawn from the top of the cumene recycle column T2, and 6 is a heavy component impurity stream withdrawn from the bottom of the cumene recycle column T2.
In fig. 1, a mixture containing cumene is first fed to a cumene recovery column T1 for separation, a high purity cumene stream 3 is taken from the side, a stream 2 containing hydrogen and methane is taken from the top of the column, and a stream 4 containing cumene, AMS, DMBA and polymer is taken from the bottom of the column. Stream 4 enters a cumene recycle column T2, stream 5 containing recycled cumene is extracted from the top of the column and recycled to a cumene recovery column T1, and stream 6 containing heavy component impurities is extracted from the bottom of the column. Wherein the condenser, reboiler and overhead reflux streams of each column are omitted.
Fig. 2 shows a process flow diagram of a comparative example, wherein the cumene column T1 is an atmospheric column, 1 is a fresh stream of a mixture containing cumene, 2 is a stream of light component impurities taken from the top of the cumene column T1, 3 is a stream of side draw of the cumene column T1, and 4 is a stream of heavy component impurities taken from the bottom of the cumene column T1.
In fig. 2, a mixture containing cumene first enters a cumene recovery column T1 for separation, a light component impurity stream 2 is taken from the top of the column, a high purity cumene stream 3 is taken from the side, and a stream 4 containing cumene, AMS, DMBA and polymer is taken from the bottom of the column. Wherein the condenser, reboiler and overhead reflux streams of each column are omitted.
Detailed Description
While the present invention will be described in detail with reference to the following examples, it should be understood that the following examples are illustrative of the present invention and are not to be construed as limiting the scope of the present invention.
[ example 1 ]
The discharge flow of the benzyl alcohol conversion reactor was 8kg/h, with a cumene content of 97.94%, a hydrogen content of 0.02 wt%, a methane content of 0.01 wt%, an AMS content of 0.25 wt%, a DMBA content of 0.06 wt%, a polymer content of 1.15 wt%, and the balance other impurities. The technical method of figure 1 is adopted to carry out impurity removal treatment on the discharged material of the benzyl alcohol conversion reactor, and high-purity isopropyl benzene is obtained at the same time.
The operation pressure of the cumene recovery tower is 0.04MPaG, the tower top temperature is 142 ℃, the tower bottom temperature is 184 ℃, the number of the tower plates is 54, the feed is carried out on 36 tower plates, and the cumene is extracted from the 10 th tower plate. The cumene recycle column was operated at-0.08 MPaG, top temperature 102 ℃, bottom temperature 175 ℃, theoretical plate 16, and fed on 8 plates.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.64 percent, the cumene recovery rate R is 99.99 percent, and the light component impurity removal rate W is199.95 percent, and the removal rate W of heavy component impurities2The content was 99.64%.
[ example 2 ]
The starting materials were as in example 1.
The cumene recovery column was operated at 0.03MPaG, 136 ℃ overhead temperature, 179 ℃ column bottom temperature, 48 plates, with feed on 27 plates and cumene taken from the 15 th plate. The cumene recycle column was operated at-0.07 MPaG, 116 ℃ overhead, 188 ℃ bottom and 14 theoretical plates and fed on 6 plates. The procedure was carried out in the same manner as in example 1 except for the above-mentioned conditions.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.65 percent, the cumene recovery rate R is 99.99 percent, and the light component impurity removal rate W is199.99 percent, and the removal rate W of heavy component impurities2The content was 99.33%.
[ example 3 ]
The starting materials were as in example 1.
The cumene recovery column was operated at a pressure of 0.06MPaG, a column top temperature of 142 deg.C, a column bottom temperature of 193 deg.C, and a number of plates of 52, and fed on 35 plates, and cumene was taken from the 20 th plate. The cumene recycle column was operated at-0.06 MPaG, a top temperature of 127 deg.C, a bottom temperature of 199 deg.C, and theoretical plates of 15, and fed over 7 plates. The procedure was carried out in the same manner as in example 1 except for the above-mentioned conditions.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.77 percent, the cumene recovery rate R is 99.93 percent, and the light component impurity removal rate W is199.90 percent, and the removal rate W of heavy component impurities2The content was 99.80%.
[ example 4 ]
The starting materials were as in example 1.
The operation pressure of the cumene recovery tower is 0.08MPaG, the tower top temperature is 145 ℃, the tower bottom temperature is 190 ℃, the number of tower plates is 54, feeding is carried out on 37 tower plates, and the cumene is extracted from the 30 th tower plate. The cumene recycle column was operated at-0.05 MPaG, 128 ℃ overhead, 198 ℃ bottom and 14 theoretical plates and fed over 6 plates. The procedure was carried out in the same manner as in example 1 except for the above-mentioned conditions.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the purity of the cumene is 99.69 percent, the recovery rate R of the cumene is 99.87 percent, and the removal rate W of light component impurities199.89 percent, and the removal rate W of heavy component impurities2The content was 99.91%.
[ example 5 ]
The starting materials were as in example 1.
The operation pressure of the cumene recovery tower is 0.10MPaG, the temperature of the tower top is 146 ℃, the temperature of the tower bottom is 195 ℃, the number of the fillers is 6, the materials are fed between the 4 th section of the fillers and the 5 th section of the fillers, and the cumene is extracted from the middle of the 3 rd section of the fillers and the 4 th section of the fillers. The operation pressure of the cumene circulation tower is-0.04 MPaG, the tower top temperature is 134 ℃, the tower bottom temperature is 204 ℃, the number of the packing is 2 sections, and the packing is fed between the 1 st section and the 2 nd section. The procedure was carried out in the same manner as in example 1 except for the above-mentioned conditions.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the purity of the cumene is 99.62 percent, the recovery rate R of the cumene is 99.83 percent, and light component impurities are removedRate W199.88 percent, and the removal rate W of heavy component impurities2The content was 99.99%.
[ example 6 ]
The starting materials were as in example 1.
The cumene recovery column was operated at a pressure of 0.15MPaG, a column top temperature of 148 ℃, a column bottom temperature of 217 ℃ and a number of trays of 65, and fed on 41 trays, and cumene was taken from 30 th tray. The cumene recycle column was operated at-0.01 MPaG, 160 ℃ overhead temperature, 229 ℃ bottom temperature, 10 theoretical plates and fed on 5 plates. The procedure was carried out in the same manner as in example 1 except for the above-mentioned conditions.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.59 percent, the recovery rate R of the cumene is 99.77 percent, the removal rate W1 of light component impurities is 99.88 percent, and the removal rate W2 of heavy component impurities is 99.89 percent.
[ COMPARATIVE EXAMPLE 1 ]
The starting materials were as in example 1.
The discharge flow of the benzyl alcohol conversion reactor was 8kg/h, with a cumene content of 97.94%, a hydrogen content of 0.02 wt%, a methane content of 0.01 wt%, an AMS content of 0.25 wt%, a DMBA content of 0.06 wt%, and a polymer content of 1.15 wt%. The discharged material of the benzyl alcohol conversion reactor is subjected to heavy component removal treatment by adopting the technical method of FIG. 2.
The cumene recovery column was operated at 0.00MPaG, 150 ℃ overhead temperature, 242 ℃ bottom temperature, 52 trays, and fed on 36 trays, and cumene was taken from the 25 th tray.
The cumene recovery tower is an atmospheric tower, and the distillate at the bottom of the tower contains cumene, so that the cumene is lost. Meanwhile, the temperature of the tower kettle is higher, the energy consumption for separation is increased, and the possibility of polymerization reaction between AMS and cumene is increased. After separation by a cumene tower T1, the cumene purity is 99.45 percent, the cumene recovery rate R is 99.21 percent, and the light component impurity removal rate W199.81%, and the removal rate W of heavy component impurities2It was 95.21%.
[ COMPARATIVE EXAMPLE 2 ]
The procedure of example 1 was repeated except that: a cumene circulating tower is not adopted, namely cumene is adopted on the inner side line of the cumene recovery tower, light components are removed from the tower top, and heavy components are removed from the tower bottom.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.63 percent, the recovery rate R of the cumene is 92.82 percent, and the removal rate W of light component impurities199.95 percent, and the removal rate W of heavy component impurities2The content was 99.67%.
[ COMPARATIVE EXAMPLE 3 ]
The procedure of example 1 was repeated except that: cumene was taken from the 5 th tray with other conditions unchanged.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.44 percent, the cumene recovery rate R is 99.98 percent, and the light component impurity removal rate W is199.96 percent, and the removal rate W of heavy component impurities2The content was 99.55%.
[ COMPARATIVE EXAMPLE 4 ]
The procedure of example 1 was repeated except that: cumene was taken from the 40 th tray under otherwise unchanged conditions.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.12 percent, the cumene recovery rate R is 99.65 percent, and the light component impurity removal rate W is199.93 percent, and the removal rate W of heavy component impurities2The content was 99.57%.
[ COMPARATIVE EXAMPLE 5 ]
The procedure of example 1 was repeated except that: the operating pressure of the cumene recycle column was 0.04 MPaG; other conditions were unchanged.
After two times of separation by a cumene recovery tower T1 and a cumene circulating tower T2, the cumene purity is 99.64 percent, the cumene recovery rate R is 99.99 percent, and the light component impurity removal rate W is199.95 percent, and the removal rate W of heavy component impurities2The content was 99.65%. At the moment, the temperature of the top of the cumene circulation tower is 169 ℃, the temperature of the bottom of the cumene circulation tower is 248 ℃, the possibility of polymerization reaction between AMS and cumene is increased, polymers can be accumulated in the system, catalyst pore passages and equipment pipelines are blocked, and the activity and the reaction rate of the catalyst are influencedAnd (4) equipment safety. Meanwhile, the polymer has a high boiling point, and the load of equipment is easily increased after the polymer is formed in a system.
Any numerical value mentioned in this specification, if there is only a two unit interval between any lowest value and any highest value, includes all values from the lowest value to the highest value incremented by one unit at a time. For example, if it is stated that the amount of a component, or a value of a process variable such as temperature, pressure, time, etc., is 50 to 90, it is meant in this specification that values of 51 to 89, 52 to 88 … …, and 69 to 71, and 70 to 71, etc., are specifically enumerated. For non-integer values, units of 0.1, 0.01, 0.001, or 0.0001 may be considered as appropriate. These are only some specifically named examples. In a similar manner, all possible combinations of numerical values between the lowest value and the highest value enumerated are to be considered to be disclosed in this application.
It should be noted that the above-mentioned embodiments are only for explaining the present invention, and do not constitute any limitation to the present invention. The present invention has been described in relation to an exemplary embodiment, and it is understood that the words which have been used herein are words of description and illustration, rather than words of limitation. The invention can be modified, as prescribed, within the scope of the claims and without departing from the scope and spirit of the invention. Although the invention has been described herein with reference to particular means, materials and embodiments, the invention is not intended to be limited to the particulars disclosed herein, but rather extends to all other methods and applications having the same functionality.
Claims (16)
1. A method for refining isopropyl benzene comprises the following steps:
step 1, rectifying a stream containing cumene, discharging light components from the top of a tower, and extracting the cumene from a side line;
and 2, further rectifying the tower bottom liquid obtained in the step 1, circulating the tower top stream to the step 1 as a raw material, and discharging the tower bottom liquid.
2. The refining method as claimed in claim 1, wherein the stream containing cumene of step 1 is a reaction product of α, α dimethyl benzyl alcohol and hydrogen gas in the preparation of propylene oxide by the cumene hydroperoxide process.
3. The refining method of claim 1, wherein the stream containing cumene in step 1 contains cumene, light component impurities and heavy component impurities;
preferably, in the stream containing cumene, the weight contents of the components are: the cumene content is 90-100 wt%, the light component impurity content is 0-2.5 wt%, and the heavy component impurity content is 0-7.5 wt%.
4. The refining method according to claim 1, wherein in step 1, the pressure of the rectification treatment is controlled to be 0.01 to 0.15MPaG, preferably 0.03 to 0.12 MPaG.
5. The refining method according to claim 1,
in the rectification treatment in the step 1, the temperature of the top of the tower is controlled to be 100-210 ℃, and preferably 120-180 ℃; and/or the presence of a gas in the gas,
in the rectification treatment in the step 1, the temperature of a tower kettle is controlled to be 130-280 ℃, and preferably 160-260 ℃.
6. The refining method according to claim 1, wherein the rectification in step 1 is carried out with a theoretical plate number of 20 to 70, preferably 30 to 60;
preferably, the cumene is sidetrack-withdrawn at a theoretical plate of 10 to 30, preferably 15 to 25; and/or at a theoretical plate of 25 to 41, preferably 30 to 35.
7. The refining method according to any one of claims 1 to 6, wherein the rectification in step 2 is performed under vacuum, and preferably the pressure in the rectification in step 2 is controlled to be-0.09 to-0.01 MPaG, and more preferably-0.09 to-0.04 MPaG.
8. The refining method according to claim 7, wherein in the rectification treatment in the step 2, the temperature of the top of the tower is controlled to be 80 to 160 ℃, preferably 100 to 150 ℃, and/or the temperature of the bottom of the tower is controlled to be 150 to 240 ℃, preferably 140 to 230 ℃.
9. The refining method according to claim 8,
when the rectification in the step 2 is carried out, the number of theoretical plates is 10-50, preferably 10-30; and/or the presence of a gas in the gas,
when the rectification in the step 2 is carried out, feeding is carried out at a theoretical plate number of 5-20, and preferably at a theoretical plate number of 5-10.
10. The cumene refining system sequentially comprises a cumene recovery tower and a cumene circulating tower according to a feeding sequence, wherein a cumene lateral line extraction position is arranged at the middle upper part of the cumene recovery tower, a tower kettle of the cumene recovery tower is connected with a feeding hole of the cumene circulating tower, and the tower top of the cumene circulating tower is connected with the feeding hole of the cumene recovery tower.
11. The system according to claim 10, wherein the cumene recovery column and/or the cumene recycle column is selected from a rectification column, preferably the cumene recovery column is an atmospheric rectification column and the cumene recycle column is a vacuum rectification column.
12. The system of claim 10,
the theoretical plate number of the cumene recovery tower is 20-70, preferably 30-60; and/or
The theoretical plate number of the cumene circulation tower is 10-50, and preferably 10-30.
13. The system of claim 12,
in the cumene recovery tower, a cumene side-draw position is arranged at a theoretical plate position of 10-30, preferably 15-25; and/or the presence of a gas in the gas,
feeding at a theoretical plate of 25-41, preferably 30-35 of the cumene recovery column; and/or
A light component outlet is arranged at the top of the cumene recovery tower; and/or
And a heavy component outlet is arranged at the tower kettle of the cumene recovery tower and is connected with a feed inlet of the cumene circulating tower.
14. The system of claim 12,
feeding at a theoretical plate of 5-20 of the cumene circulation tower, preferably at a theoretical plate of 5-10; and/or
And a circulating cumene outlet is arranged at the top of the cumene circulating tower and is connected with a feed inlet of the cumene recovery tower.
15. The system according to any one of claims 10 to 14,
the pressure of the cumene recovery tower is 0.01-0.15 MPaG, preferably 0.03-0.12 MPaG; and/or
The temperature of the top of the cumene recovery tower is 100-210 ℃, preferably 120-180 ℃, and/or
The temperature of a tower kettle of the cumene recovery tower is 130-280 ℃, and preferably 160-260 ℃.
16. The system of claim 15,
the cumene circulation tower is a vacuum tower, and the pressure of the cumene circulation tower is preferably-0.09 to-0.01 MPaG, and more preferably-0.09 to-0.04 MPaG; and/or
The tower top temperature of the cumene circulation tower is 80-160 ℃, and preferably 100-150 ℃; and/or the presence of a gas in the gas,
the temperature of a tower kettle of the cumene circulating tower is 150-240 ℃, and preferably 140-230 ℃.
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